US3428654A - Alkene sulfonation process and products - Google Patents

Alkene sulfonation process and products Download PDF

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Publication number
US3428654A
US3428654A US548827A US54882766A US3428654A US 3428654 A US3428654 A US 3428654A US 548827 A US548827 A US 548827A US 54882766 A US54882766 A US 54882766A US 3428654 A US3428654 A US 3428654A
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Prior art keywords
olefin
sulfuric acid
product
stage
treatment
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US548827A
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Joseph Rubinfeld
Willem Bian Gwan Ouw
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Colgate Palmolive Co
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Colgate Palmolive Co
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Priority to ZA672362D priority Critical patent/ZA672362B/xx
Application filed by Colgate Palmolive Co filed Critical Colgate Palmolive Co
Priority to US548827A priority patent/US3428654A/en
Priority to ES0328934A priority patent/ES328934A1/es
Priority to FR70039A priority patent/FR1489920A/fr
Priority to SE10100/66A priority patent/SE347256B/xx
Priority to CH1075566A priority patent/CH491875A/de
Priority to DE1568311A priority patent/DE1568311B2/de
Priority to GB34589/66A priority patent/GB1166857A/en
Priority to GB20245/69A priority patent/GB1166858A/en
Priority to BE685012D priority patent/BE685012A/xx
Priority to DK403866AA priority patent/DK130787B/da
Priority to JP41050842A priority patent/JPS4935609B1/ja
Priority to SE06929/67A priority patent/SE336866B/xx
Priority to FR107772A priority patent/FR92528E/fr
Priority to DE1617064A priority patent/DE1617064B2/de
Priority to BE699149D priority patent/BE699149A/xx
Priority to GB24863/67A priority patent/GB1194862A/en
Priority to ES341149A priority patent/ES341149A2/es
Priority to CH764067A priority patent/CH496086A/de
Priority to DK285067AA priority patent/DK128906B/da
Application granted granted Critical
Publication of US3428654A publication Critical patent/US3428654A/en
Priority to SE15191/69A priority patent/SE350507B/xx
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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D3/00—Other compounding ingredients of detergent compositions covered in group C11D1/00
    • C11D3/16—Organic compounds
    • C11D3/34—Organic compounds containing sulfur
    • C11D3/3472—Organic compounds containing sulfur additionally containing -COOH groups or derivatives thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
    • C07C2/66—Catalytic processes
    • C07C2/68—Catalytic processes with halides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C309/00—Sulfonic acids; Halides, esters, or anhydrides thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C309/00—Sulfonic acids; Halides, esters, or anhydrides thereof
    • C07C309/01—Sulfonic acids
    • C07C309/02—Sulfonic acids having sulfo groups bound to acyclic carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C309/00—Sulfonic acids; Halides, esters, or anhydrides thereof
    • C07C309/01—Sulfonic acids
    • C07C309/62—Sulfonated fats, oils or waxes of undetermined constitution
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09B—ORGANIC DYES OR CLOSELY-RELATED COMPOUNDS FOR PRODUCING DYES, e.g. PIGMENTS; MORDANTS; LAKES
    • C09B1/00—Dyes with anthracene nucleus not condensed with any other ring
    • C09B1/16—Amino-anthraquinones
    • C09B1/20—Preparation from starting materials already containing the anthracene nucleus
    • C09B1/22—Dyes with unsubstituted amino groups
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09B—ORGANIC DYES OR CLOSELY-RELATED COMPOUNDS FOR PRODUCING DYES, e.g. PIGMENTS; MORDANTS; LAKES
    • C09B1/00—Dyes with anthracene nucleus not condensed with any other ring
    • C09B1/50—Amino-hydroxy-anthraquinones; Ethers and esters thereof
    • C09B1/503—Amino-hydroxy-anthraquinones; Ethers and esters thereof unsubstituted amino-hydroxy anthraquinone
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/02—Anionic compounds
    • C11D1/12—Sulfonic acids or sulfuric acid esters; Salts thereof
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/02—Anionic compounds
    • C11D1/12—Sulfonic acids or sulfuric acid esters; Salts thereof
    • C11D1/14—Sulfonic acids or sulfuric acid esters; Salts thereof derived from aliphatic hydrocarbons or mono-alcohols
    • C11D1/143—Sulfonic acid esters
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/02—Anionic compounds
    • C11D1/37—Mixtures of compounds all of which are anionic
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/66—Non-ionic compounds
    • C11D1/83—Mixtures of non-ionic with anionic compounds
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/88—Ampholytes; Electroneutral compounds
    • C11D1/94—Mixtures with anionic, cationic or non-ionic compounds
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D3/00—Other compounding ingredients of detergent compositions covered in group C11D1/00
    • C11D3/0005—Other compounding ingredients characterised by their effect
    • C11D3/0026—Low foaming or foam regulating compositions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • C07C2527/06—Halogens; Compounds thereof
    • C07C2527/125—Compounds comprising a halogen and scandium, yttrium, aluminium, gallium, indium or thallium
    • C07C2527/126—Aluminium chloride
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/02—Anionic compounds
    • C11D1/12—Sulfonic acids or sulfuric acid esters; Salts thereof
    • C11D1/14—Sulfonic acids or sulfuric acid esters; Salts thereof derived from aliphatic hydrocarbons or mono-alcohols
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/02—Anionic compounds
    • C11D1/12—Sulfonic acids or sulfuric acid esters; Salts thereof
    • C11D1/22—Sulfonic acids or sulfuric acid esters; Salts thereof derived from aromatic compounds
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/02—Anionic compounds
    • C11D1/12—Sulfonic acids or sulfuric acid esters; Salts thereof
    • C11D1/29—Sulfates of polyoxyalkylene ethers
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/38—Cationic compounds
    • C11D1/52—Carboxylic amides, alkylolamides or imides or their condensation products with alkylene oxides
    • C11D1/523—Carboxylic alkylolamides, or dialkylolamides, or hydroxycarboxylic amides (R1-CO-NR2R3), where R1, R2 or R3 contain one hydroxy group per alkyl group
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/38—Cationic compounds
    • C11D1/62—Quaternary ammonium compounds
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/66—Non-ionic compounds
    • C11D1/72—Ethers of polyoxyalkylene glycols
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/66—Non-ionic compounds
    • C11D1/75—Amino oxides
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/88—Ampholytes; Electroneutral compounds
    • C11D1/90—Betaines

Definitions

  • This invention relates to production of sulfonic acids and relates more particularly to the production of detergents.
  • the sulfonation reaction is typically carried out by bringing a stream of sulfur trioxide, highly diluted with an inert gas such as air, into contact with the alphaolefin to produce a viscous acidic product which is believed to contain :alkene 'sulfonic acids and sultones (which are cyclic compounds containing an OSO group attached to two carbon atoms, which carbon atoms are connected to each other either directly or through intervening carbon atoms); according to the aforesaid Dutch patent, the product contains about unsaturated sulfonic acid and 65% sultone.
  • R R R CCH CH CH +SO products such as alkene sulfonic acids:
  • R is an alkyl radical and R and R are alkyl or hydrogen.
  • the sulfonated product is then hydrolyzed and neutralized, as by treatment with strong aqueous alkali; during this procedure hydrolysis of the sultones is effected to produce hydroxyalkanesulfonic acids.
  • the resulting neutralized product has relatively low detergent power. Its detergent power can be improved to some extent by deoiling to remove the significant amount (e.g. 15-25% based on the total organic content) of water-insoluble material. Such de-oiling is an expensive and wasteful process and its use substantially increases the cost of the 3,428,654 Patented Feb. 18, 1969 detergent material and the capital investment which would be required for detergent production.
  • One feature of this invention relates to the use of strong sulfuric acid to treat a sulfonation product of an olefin.
  • Treatment with the sulfuric acid in accordance with this invention has been found to greatly decrease the ratio of water-insoluble pentane-soluble organic material to active organic detergent material in the product, e.g. decreasing this ratio by more than one-half, e.g., by more than
  • the extent of the reduction will depend, all other things being equal, on the amount of unreactive alkanes and other types of saturated or unreactive materials present as impurities in the starting olefin.
  • the ratio of the water-insoluble pentane-soluble organic material (often termed free oil) to the active sulfonated organic detergent material in the resulting product is generally less than 1:10 and preferably less than 0.7110 (e.g., in the range of 02:10 to 0.7210) and the product may, after a simple treatment with base, be used directly as a detergent of properties equal to, or better than, those of standard commercial detergents, without any de-oiling treatment.
  • the process of this invention may be applied to olefin feed mixture having relatively high contents of alkanes and other types of saturated or unreactive materials to yield products which are surprisingly effective as detergents, even though they contain large amounts of free oil. While the presence of the unreacted alkane in the product reduces the foaming qualities of the detergent, it does not have any significant detrimental effect on its detersive power. In these products the ratio of the amount of non-alkane materials in the free oil to the amount of active sulfonated detergent material is very low, i.e., on the same order as the corresponding ratio in the detergent products made from the purer olefin cuts.
  • the free oil content of the products may be further reduced by a special heat-treatment, as described in our copending application Ser. No. 548,826, entitled Heat- Treatment of Sulfonated Olefin Products, which was filed on even date herewith and whose disclosure is incorporated herein by reference.
  • the product is unique in its overall characteristics and properties which make it particularly suitable in the formulation of detergent compositions. As indicated, it exhibits many technical advantages including highly desirable detergent efiiciency combined with other special characteristics such as foaming power, emulsification power or ability, etc.
  • the olefin or alkene may be an aliphatic unsaturated hydrocarbon, containing from about 5 to 30 carbon atoms and having the structure (wherein R and R have the meaning previously given.
  • R and R have the meaning previously given.
  • We may use mixtures which contain alkenes of various molecular weights, e.g., mixtures containing straight chain primary alkenes.
  • alkenes for use in the sulfonation process are amylene, hexene, nonene, dodecene, tetradecene, hexadecene, heptadecene, octodecene, docosene, pentacosene, and the like, as well as mixtures of said alkenes.
  • a preferred alkene for use in the present invention is an alkene or olefin having a terminal double bond and an essentially acyclic straight-chain structure which contains about 8 to 25 carbon atoms in the molecule.
  • These a-olefins or l-olefins may consist essentially of a single compound or mixtures of said compounds, although the olefin feed also may contain secondary or internal olefins, diolefins, cyclic olefins, aromatics, naphthenes, and as indicated above, alkanes.
  • a particularly preferred olefin feedstock contains in the range of about 12 to 21 carbon atoms in the molecule and yields alkenyl sulfonates having excellent detergency properties.
  • the alkene or olefin feed materials may be derived from primary, secondary and tertiary alcohols by dehydration, or from halogenated hydrocarbons by dehalogenation, or from saturated hydrocarbons through cracking or catalytic dehydrogenation or by polymerization of olefins such as ethylene, butylene, propylene and the like. Particularly satisfactory materials may be obtained by cracking petroleum wax or catalytic polymerization of ethylene. The latter processes produce essentially acylic straight-chain compounds which upon sulfonation and neutralization result in readily biodegradable alkene sulfonates. Another method of making the alkene is by dehydration of long chain fatty alcohols.
  • the initial sulfonation reaction involves treatment of the olefin with sulfur trioxide, and may be carried out in a manner known in the art, as by feeding a stream of sulfur trioxide highly diluted with inert gas (e.g., an inert gas: S mole [volume] ratio of :1 to 100:1, preferably less than about :1, e.g., 50:1 to 20:1) into contact with a stream of the olefin feedstock.
  • inert gas e.g., an inert gas: S mole [volume] ratio of :1 to 100:1, preferably less than about :1, e.g., 50:1 to 20:1
  • the mole ratio of S0 to olefin is advantageously about 1:1; that is, about one mole of S0 is absorbed per mole of olefin feed.
  • the amount of sulphonic acid in the intermediate product is somewhat higher than that obtained at 1:1 ratios but the final product is considerably more darkly colored.
  • the inert gases which may be used for dilution of the sulfur trioxide are air and nitrogen, which are preferred, carbon dioxide, sulfur dioxide, low molecular weight paraflinic hydrocarbons, etc.
  • the gaseous sulfur trioxide may be provided by vaporizing a stabilized liquid sulfur trioxide or by using converter gas obtained from a sulfur burner. Undiluted S0 e.g., at low subatmospheric pressures corresponding to the S0 partial pressures in the SO -diluent mixtures, may be used.
  • liquid sulfur trioxide When liquid sulfur trioxide is used as the sulfonating agent, it is preferred to use a liquid diluent such as sulfur dioxide, carbon tetrachloride, hexane, etc. to minimize local overheating and prevent undesirable side reactions such as oxidation and polymerization.
  • a liquid diluent such as sulfur dioxide, carbon tetrachloride, hexane, etc.
  • the olefin In carrying out the initial SO -olefin reaction, it is advantageous to maintain intimate contact between a supply of gaseous S0 and the olefin. This may be conveniently effected in a continuous manner by exposing to the S0 one or both faces of a thin flowing film of olefin, as by passing the thin film of olefin down the wall of a tube into the inner portion of which the S0 is injected.
  • the olefin passes continuously through an annular zone between the outer surface of a cylindrical rotor and the inner wall of a cylindrical vessel coaxial therewith, while the diluted S0 is injected into that zone from many ports spaced along the length and around the circumference of that zone.
  • the S0 may be injected into a dominant liquid bath of the olefin maintained under vigorously agitated or turbulent conditions, or fine droplets of the olefin may be dispersed in a gaseous stream of S0 and inert gas. Continuous sulfonation is presently preferred over batch processing, because it has thus far given improved efficiency and higher quality products.
  • the temperature is advantageously maintained below C., a temperature of less than about 50 C. and, when feasible, not above about 40 C. (e.g. within the range of about 10-40" C.) being preferred. It is usually desirable to Work at a temperature at which the sulfonated material produced by the reaction remains in liquid condition. Accordingly, the choice of a particular temperature is in part dependent on the particular olefin used, since the sulfonated products of higher molecular weight, e.g., those made from C olefins, will tend to precipitate out of the mixture more readily, at low temperatures, than the lower molecular weight sulfonated products (e.g.
  • cooling may be effected by passmg a cooling medium, such as water, through a jacket surrounding the tubular reactor in which the SO -olefin reaction takes place.
  • the gaseous effi uent leaving the reactor after the contact between the S0 and olefin is generally substantially free of S0 and consists practically entirely of the inert gas, together with a very small amount of S0 and some entrained reaction mixture.
  • Stage I mix The product of the initial sulfonation reaction (herelnafter termed Stage I mix, for convenience) is usually a dark brown viscous material, having an appearance similar to a melted chocolate bar.
  • Typical Stage I mixes made with a 1:1 SO :olefin mole ratio, contain in the neighborhood of about 35 mole percent active ingredients (based on moles of olefin and measured by titration of the acidic mix with a standard cetyl trimethylammonium bromide solution); on heating with aqueous caustic, to effect neutralization of the sulfonic acids and hydrolysis, by ring-opening, of some of the sultones, this proportion rises to about or higher.
  • the neutralization and hydrolysis reaction requires an extended period of time; if the sulfonation product is heated with aqueous sodium hydroxide for a shorter period, e.g., a half-hour at 98 C., to produce a material having a neutral or basic pH, the pH changes on storage and the material may become strongly acidic on standing for several days.
  • sulfuric acid is incorporated into the Stage I mix.
  • the sulfuric acid is supplied as a separate steam, being added as an aqueous solution (e.g., a 60% sulfuric acid solution) or as 100% sulfuric acid or as oleum (e.g., 65% oleum). 20% oleum has given excellent results, as has sulfuric acid supplied as a 90% or 97% solution; the latter are preferred over the oleum because of economy in use of material and production of lighter colored products.
  • the optimum quantity of sulfuric acid incorporated in this stage of the process is dependent on the reaction conditions in this stage and in the initial stage.
  • the amount of added sulfuric acid will be in the range of about 2 to 300 parts by weight per 100 parts of Stage I mix.
  • the amount of added sulfuric acid is preferably in the range of 2 to 100, e.g., 2 to 50 parts by weight per 0 parts by weight of Stage I mix.
  • the amount of water supplied in the added acid is small, e.g., less than 10% of the weight of the Stage I mix; in the preferred process it is less than 5%, usually less than 3%.
  • the sulfuric acid treatment takes place under substantially non-hydrolyzing conditions, in contrast to treatment in dilute aqueous medium.
  • the sulfuric acid treatment is preferably effected at a temperature sufficient to keep the mixture in a fiowable state.
  • the temperatures may, for example, be in the range of about 10 to 100 0., preferably in the range of about 25 to 60 C.
  • the duration of the sulfuric acid treatment is advantageously relatively short, preferably less than about an hour, best results being obtained with times of less than about 20' minutes, e.g., 5 minutes or less.- Good results have been obtained even when the sulfuric acid was injected into the Stage I mix less than one minute before the mixture was brought into contact with an alkaline neutralizing agent (e.g. excess aqueous NaOH); in one run the Stage I mix was blended with the sulfuric acid and heated to about 55 C. during a period of about 13 seconds and then directly neutralized.
  • an alkaline neutralizing agent e.g. excess aqueous NaOH
  • the addition of the sulfuric acid may be effected in any suitable apparatus, preferably one in which the ingredients are mixed together thoroughly and quickly.
  • One suitable technique for continuous operation is to feed the Stage I mix and sulfuric acid to a recycle loop.
  • This may be a continuous loop of tubing having a inlet at one point through which the ingredients are fed continuously (preferably a pump to which both the Stage I mix and sulfuric acid are supplied continuously), and an outlet, at another point, through which the product is removed continuously, the total rates of feed and withdrawal (which are substantially equal) being each only a fraction (e.g. less than /s) of the rate at which the mixture is passed through the loop; thus the material recycles many times in the loop and the composition of the withdrawn material is substantially the same as that of the material circulating throughout the loop.
  • the sulfuric acid treatment is an exothermic reaction; if desired, the
  • the appearance of the sulfuric acid-treated material is similar to that of the Stage I mix; that is, it is a viscous dark material, again like a melted chocolate bar.
  • the treated material is preferably fed directly into contact with a basic material to neutralize it. It is, however, within the broader scope of this invention to give the material an intermediate treatment, preferably a thermal treatment, which may be effected in aqueous medium, prior to neutralization.
  • an intermediate treatment preferably a thermal treatment, which may be effected in aqueous medium, prior to neutralization.
  • the material may be mixed with water, or with dilute sulfuric or other acid, and heated (e.g., to C. or higher, e.g. 200 C. under superatmospheric pressure) before neutralizing it my contact with a basic material.
  • the treatment with base may be carried out on a batch or continuous scale.
  • it is effected by thoroughly mixing the acidic product with a basic material and water, eg with a 10*, 20, 30, 40 of 50% aqueous solution of sodium hydroxide and, conveniently, maintaining the mixture at an elevated temperature above 60 C., e.g. in the range of about 65200 C. (using superatmospheric pressures for the higher temperatures, when needed), preferably in the range of about 90-100 C.
  • the neutralization goes to completion much more rapidly for the sulfuric acid treated material than for the Stage I mix, previously described. Neutralization times well under an hour may be employed, e.g., /2 hour or less without the danger of the gradual auto-acidification of the product on storage.
  • the alkali is used in amount such that the pH of the resulting aqueous solution is about 10 or higher; this makes for easier manufacturing control than the use of an amount precisely sufficient to give a pH of 7 or 8.
  • the sulfuric acid treatment is effected under such conditions as to produce a treated material having a very low sultone content
  • the alkali treatment conditions are preferably made less drastic; for example, the alkali treatment may be effected at room temperature with short contact times.
  • the product of the aqueous base treatment is generally a syrupy liquid
  • the starting olefin includes an appreciable proportion of olefins of less than eighteen (e.g., 15) carbon atoms.
  • olefins of less than eighteen (e.g., 15) carbon atoms.
  • suitable mixtures e.g., obtained from feeds comprising C C olefin mixtures or C C olefin mixtures
  • freeflowing viscous syrups free of solid particles are obtained even at high solids contents (well above 40%, e.g., at 60% solids).
  • reaction mixture in the sulfuric acid treatment, which is effected in the presence of little or no water, the reaction mixture is much less corrosive than sulfuric acid-containing mixtures in which large amounts of water are present. This makes it possible to carry out the sulfuric acid treatment in ordinary steel equipment. Also, the reaction mixture is generally substantially free of HCl or other corrosive chlorides.
  • the neutralization products produced in accordance with this invention generally contain minor proportions of hydroxysulfonates, which may be present owing to incomplete conversion of sultone during the sulfuric acid treatment and resultant hydrolysis of the sultone to hydroxysulfonate.
  • the proportions of hydroxysulfonate are well below those reported in the literature; thus, the Dutch patent previously cited refers to the conversion of the 65% sultone content to hydroxysulfonate, Kaiser and Puschel, Chem. Ber. 97 (1964), page 2929, state that gamma sultone is converted, on hydrolysis, 67% to hydroxyalkane sulfonate, and British Patent 983,056 (pub. Feb.
  • Oxidative cleavage studies of the neutralized product indicate that its alkenyl sulfonates are predominantly A-3,4; for example, oxidative cleavage studies made on the alkenyl sulfonates obtained on sulfonation, in accordance with this invention, of an olefin cut consisting substantially completely of C hydrocarbons indicate that, of the total alkenyl sulfonates, about 6570% Was A-3,4, about 10-13% was A-4,5 and about 1013% was A-2,3.
  • the unsulfonated hydrocarbons remaining in the products of this invention usually have a relatively low olefin content.
  • the olefin content of these unsulfonated hydrocarbons is well below 60%, and is made up principally of trans olefins, as demonstrated by infrared spectrographic analysis, and the total hydrocarbon content of the neutralized product is below about 5% (on an organic dry basis).
  • the total amount of hydrocarbons in the neutralized product is correspondingly higher due to the presence of unreacted paraffins, and the relative proportion of olefins to total hydrocarbons is correspondingly lower.
  • the hydrocarbons constituted over of the total free oil, the other constituents being sulfur-containing intermediates, and paraffins constituted the major portion of these hydrocarbons.
  • the color of the material produced in accordance with this invention will depend in part on the impurities in the feedstock.
  • feedstocks such as certain relatively unrefined cracked paratfin waxes (which feedstocks, although high in alpha olefins, have substantial alkane contents) are changed from their original yellow color to a dark brown on contact with a single drop of S0 (for grams of feedstock) and yield darkly colored products. This color change takes place even if the feedstock has been pretreated and decolorized with suitable adsorbents. With the more highly refined feedstocks, such as those shown in Examples 2 and 14, lighter colored products can be attained.
  • An improvement in color can also be attained by the incorporation of a small amount of an antioxidant, eg an amount in the range of about 0.01% to 1% of a phenolic antioxidant, in the olefin before or during the reaction.
  • an antioxidant eg an amount in the range of about 0.01% to 1% of a phenolic antioxidant
  • Iphol 2.6-di-tert-butylphenol
  • the color of the final neutralized product was lowered from a value of 950 Klett (obtained without the addition of the antioxidant) to a value of 350 Klett.
  • Antioxidants which react with S0 may be used, e.g. a-naphthol which is an antioxidant and reacts with S0 to form another antioxidant, namely, naphtholsulfonic acid.
  • the color of the neutralized product may also be lightened by the addition of a bleaching agent.
  • the neutralized product may be treated with sodium hypochlorite; alternatively, another oxidizing bleaching agent, such as hydrogen peroxide, may be added to the Stage II mix before or after neutralization, preferably while carefully controlling the temperature below 25 C.; aqueous H 0 e.g., of 35% concentration) may be used for this purpose.
  • the bleached product substantially retains its light color after heat-treatment; in this respect it is far superior to the products resulting from similar bleaching of the sulfonated olefin products of the prior art; additional details on this point are found in the copending application on Treatment of Detergents, previously mentioned.
  • Example 1 Using a jacketed tubular reactor having an internal diameter of 0.824 inch and a length of 194 as the first sulfonation stage, an alkene mixture having an average molecular weight of about 228 was continuously sulfonated with a gaseous mixture containing 4% by volume of sulfur trioxide in air.
  • the alkene mixture contained about 88% of terminally unsaturated straight chain olefins having a chain length of about 15 to 20 carbons (CRT-16%, G g-114%, cp -14%, C g-17%, C -21%, C 17%, approximately), 6% internally unsaturated branched and straight chain olefins, 3% diolefins and 3% alkanes (analysis by mass spectroscopy).
  • the alkene was distributed as a falling film over the inner wall of the reaction tube at the top thereof and the gaseous sulfonating agent was injected downward at a high volumetric rate into the center of the reaction tube at the top thereof.
  • Reaction temperature was controlled in the range of about F. using 5065 F. cooling water in the cooling jacket surrounding the reactor and the pressure in the reaction was about 10 p.s.i.g. About 40 9 lbs/hr. of alkene was reacted with about 14 lbs./hr. of sulfur trioxide 1:1 mole ratio of S to alkene) dispersed in 30 cu.ft./minute of air having a dew point of about 100 F. (1 ppm of water).
  • the Stage I mix from the tubular reactor was separated continuously from entrained gases in a separator at the base of the reactor and then injected continuously into a recycle loop (of the type previously described) together with 6.5 lbs/hr. of 20% oleum, both the Stage I mix and the oleum being added continuously at a pump at the inlet of the recycle loop, and the recycling mixture in the loop was maintained at a temperature of about 105 F.
  • the average residence time in the recycle loop was about 25 minutes, the pressure therein was on the order of p.s.i.g., and the material continuously leaving the recycle loop was neutralized directly with aqueous dilute sodium hydroxide at a temperature of about 180- 200 F. to a pH of 9-10.
  • Example 1 was repeated using a C alpha-olefin out which was a hydrocarbon mixture produced by anionic polymerization of ethylene and containing 93.9 mole percent olefins (of the following distribution: 1.4 mole percent C 87.6 mole percent C 4.9 mole percent C 1.2 mole percent paraffins, 4.2 mole percent diolefins, 0.05 mole percent triolefins and 0.7 mole percent aromatics (analysis by mass spec., as in Example 1), the average molecular weight of the olefins being 253.
  • a C alpha-olefin out which was a hydrocarbon mixture produced by anionic polymerization of ethylene and containing 93.9 mole percent olefins (of the following distribution: 1.4 mole percent C 87.6 mole percent C 4.9 mole percent C 1.2 mole percent paraffins, 4.2 mole percent diolefins, 0.05 mole percent triolefins and 0.7 mole percent aromatics (analysis by
  • the rate of feed of the olefin cut was about 40.5 lbs/hr. and the rate of feed of the sulfur trioxide was about 13 lbs/hr. (the S0 concentration in the air-S0 feed being about 4 volume percent).
  • the temperature in the first stage of reaction was somewhat higher than that in Example 1 (the exit temperature of the cooling water being about 85 F.). Instead of 20% oleum there was employed 90% H 50 which was supplied continuously to the recycle loop at the rate of 1.8 lbs/hr.
  • the residence time in the recycle loop was about 5 minutes, and the temperature of the material in the loop was maintained at about 115 F.
  • the neutralization was effected with 30% aqueous caustic soda solution at a temperature of 240 F. (heat being supplied by injection of live steam).
  • the slurry resulting from the neutralization had a pH of 13.5 and was analyzed, after evaporating olf most of the water, to determine the total non-volatile or solids content (determined, by difference, after removing water by azeotropic distillation with Skellysolve V, a volatile petroleum fraction).
  • This non-volatile content includes the inorganic salts, free oil, free alkali and active anionic surfactant.
  • one sample was mixed with ethanol to cause the inorganic salts to precipitate out; these were filtered oif, dried at 105 C. and weighed, and then ignited at 600 C. and again weighed; the filtrate was titrated for free alkali.
  • free oil about 0.3% free alkali (as NaOH) and about 26.8% active anionic ingredient (by difference); the cationic titration indicated an active anionic ingredient content of 25.85%.
  • the free oil content based on the total organic content (dry basis) was about 5%.
  • the sulfuric acid treatment was omitted, the free oil content, based on the total organic content, was over 15%.
  • the ethylene glycol distillable proportion of the neutralized slurry was found to be 1.04% of the total aqueous slurry, or about 3.8% of the total organic content (dry basis).
  • This analysis which was conducted, on still another sample, substantially in the manner described in the Journal of the American Oil Chemists Society, vol. 40 1963) pp. 257-260, indicates the amount of unsulfonated hydrocarbon. It will be understood that the hydrocarbon, whose content is determined in this manner, is part of the free oil. When the sulfonation was effected in a similar manner but the sulfuric acid treatment was omitted, the ethylene glycol-distillable portion was over 11% of the total organic content.
  • FIGS. 1 and 2 Infrared spectra of the free oil of this Example 2 are shown in FIGS. 1 and 2.
  • FIG. 1 which is a spectrum of semisolid film of the material, has strong hands at about 7.35-7.45 microns (doublet) and about 8.468.6 microns (doublet) indicating the presence of sultones and about 7.65 and 7.7 microns (doublet) indicating the presence of delta-sultone. It also has a band at about 10.35 microns indicating the presence of trans-olefins.
  • FIG. 1 which is a spectrum of semisolid film of the material, has strong hands at about 7.35-7.45 microns (doublet) and about 8.468.6 microns (doublet) indicating the presence of sultones and about 7.65 and 7.7 microns (doublet) indicating the presence of delta-sultone. It also has a band at about 10.35 microns indicating the presence of trans-olefins.
  • the infrared spectrum of the glycol-distillable material of this Example 2 is shown in FIG. 3, which was taken on a liquid film 0.020 mm. thick. This spectrum indicates that no significant amount of alpha-olefin is present (no absorption bands at about 11.0, 10.06, 6.06 and 3.20 microns) and that the material contains a rather large amount of trans olefin (strong band at about 10.35 microns); bands showing the presence of residual ethylene glycol (introduced in the distillation analysis), a small amount of carbonyl (5.80 microns) and saturated hydrocarbons are also present.
  • Example 3 Example 2 was repeated, but there were employed 3 lbs. per hour of the sulfuric acid, and the neutralization was effected at -200 F.
  • the free oil content of the product was about 7% of the total organic content (dry basis) while the hydrocarbon portion (that is, the glycol-distillable portion) was about 2.9% of the total organic content.
  • a mass spectrographic analysis of the glycol-distillable portion showed 50.4 mole percent monoolefin, 40.1 mole percent parafiin, 0.9 mole percent diolefin, 0.3 mole percent triolefin, 0.5 mole percent aromatic and 7.7 mole percent secondary alcohols; a similar analysis of the olefin feedstock showed 1.2 mole percent parafiins, 4.2 mole percent diolefins, 0.05 mole percent triolefins and 0.7 mole percent aromatics.
  • the infrared spectrum of the free oil of this Example 3 is illustrated in FIG. 4 (taken on a semisolid film of the material) which indicates the presence of sultones (bands at about 7.357.5 microns, about 8.48-8.6 microns) delta sultone (bands at about 7.65-7.72 microns) and trans-olefin (band at about 10.35 microns).
  • the infrared spectrum of the glycol-distillable material of this Example 3 is shown in FIG. 5 (taken on a liquid film 0.020 mm.
  • trans olefin strong band at about 10.35 microns
  • alpha olefin 11.00 micron band
  • saturated hydrocarbons and a trace of carbonyl are also present.
  • the desalted de-oiled active ingredient was dried and reacted with n-octylamine by mixing a solution of the active ingredient in alcohol with the octylamine and then evaporating the alcohol on a steam bath to recover the octylamine salt, which was then treated with heated methylene chloride.
  • Part of the actylamine salt (about 20%) crystallized out from the methylene chloride at room temperature; this insoluble material had a bromine number of zero (when tested as described later in this specification).
  • This insoluble fraction of the octylamine salt was converted to the corresponding sodium salt, whose infrared spectrum indicated that it is the same compound as the compound described in Example B below (i.e., a compound believed to be a hydroxysulfonate but not a 2-hydroxysulfonate-1). Conversion of this octylamine salt to its sodium salt was effected by treatment with an acidic cation-exchange resin followed by neutralization with NaOH.
  • Example 4 A Stage I mix, produced by use of 1 mole of S0 per mole of olefin, using the olefin mixture of Example 1, was treated with various amounts and concentrations of sulfuric acid. In each case, the sulfuric acid treatment was effected for about 5 minutes, after which the reaction product was fully neutralized by treatment with hot aqueous caustic alkali solution. The sulfuric acid was added rapidly to the Stage I mix and the blend was sheared intensively to effect thorough mixing. The results are tabulated below:
  • H2804 added in per unit of reaction the form of wt. of with sulfuric Neutralized Stage 1 acid, Unneutralizcd (hydrolyzed) mix 1 material product,
  • FIG. 6' The infrared spectrum of this crop of crystals (taken on a solid film of the material) is shown in FIG. 6', it has a broad strong band at about 8.25-8.75 microns and a medium strong band at about 9.6-9.7 microns, indicating that the material is a sulfonic acid or salt thereof.
  • the spectrum has a medium band at about 10.35 microns, indicating the presence of trans unsaturation. There is no significant absorption at about 12.65 microns, which absorption would be characteristic of alkane sulfonates and hydroxyalkanesulfonates.
  • a third fraction of the octylamine reaction product was obtained by removal of the methylene chloride from the mother liquor after the -78 C. crystallization.
  • This third fraction which constituted about 38% of the weight of the total octylamine reaction product, was a yellow wax with a bromine number of 19. Its infrared spectrum (FIG. 7, taken on a pasty film of the material) indicates that this material is a sulfonic acid or salt thereof and that it has only a small amount of trans-unsaturation (absorption at about 10.35 microns) and no alkane sulfonate or hydroxyalkanesulfonate.
  • reaction mixture was digested for 10 minutes, at 78 F. Thereafter, neutralization of the acid reaction mixture was carried out by addition of sodium hydroxide solution with agitation at a temperature of about F. to a pH within the range of 911. Residual. carbon-tetrachloride was evaporated from the aqueous sulfonate mixture. Analysis of the product showed it to contain approximately 73% of anionic active material and about 27% free oil and tar. In contrast, neutralization of the Stage I mix, without the sulfuric acid treatment, gave a product containing 37% active ingredient and 63% free oil and tar.
  • Example 6 Mole percent Ratio of free Wt. of H2804 Temperature yield (mole oil to active (anhydrous basis) of reaction percent olefin anionic ingredadded to Stage I mix with H280 converted to ient in 0. active anionic neutralized ingredient) product (a) None 47 0. 63 (b) 0.12 2025 63 4 (c) 0.24 20-25 77 2 (d) 0.36 20-25 82 18 (e) 0.3 45 81 22 (f) 0.72 45 B2 18 (g) 1.20..
  • a sample of the neutralized product of run (d) was treated to remove the free oil by taking up the product in 50% aqeuous ethanol, extracting the solution six times with redistilled petroleum ether at room temperature, and evaporating the raflinate to dryness under vacuum.
  • the infrared spectrum (FIG. 12, taken on a solid film, in a frustrated multiple internal reflection apparatus with the film on one side of the prism) of the residue shows strong absorption at about 10.7 microns and absorption at about 10.35 microns, and indicates that there is present appreciable long chain alkyl sulfate (presumably of about 18 carbon atoms, like the olefin feed), as well as trans-alkenesulfonate.
  • the isopropanol-soluble was isolated from another sample of the product of run (d) (by extracting 1 gram of sample three times, each time with 50 ml. of boiling isopropanol, and evaporating the extracts to dryness under vacuum at 60-70 C.).
  • the infrared spectrum of the product (FIG. 13, taken on a film evaporated from a methanol solution) shows the presence of long chain alkyl sulfate and alkenesulfonate but practically no sultone (i.e., well below and probably less than 5% sultone; compare the spectra of sultones shown in FIGS. 8 and 9, discussed below).
  • Example 7 An olefin out having an average molecular weight of about 224, which consisted essentially of oleflns having a chain length of 12 to 22 carbons, and containing about 92% of l-olefins and 4% of trans olefins, was given a two-stage treatment and neutralized in accordance with this invention, using a 1:1 SO :olefin mole ratio in the first stage and, in the second stage, 0.15 part by weight of 20% oleum per part of Stage I mix.
  • the neutralized product contained 97.4% active anionic ingredient and 2.6% free oil, based on total organic content (dry basis).
  • Example 8 The sulfuric acid-treated but unneutralized product of Example 1 was converted into the following salts by treatment with the corresponding hydroxides and water-soluble carbonates in stoichiometric excess in hot aqeuous solution; mercury, zinc, barium, potassium, calcium, lithium, aluminum, lead, chromium and magnesium. By reaction with aqueous ammonium hydroxide, and with triethanolamine, the corresponding ammonium and triethanol ammonium salts were also produced.
  • Example 9 The two-stage treatment was used with an olefin out having an average molecular weight of 272 and containing 91 mole percent u-olefin, of the following approximate distribution: C 3 mole percent, C 26 mole percent; C 31 mole percent; C 26 mole percent; C 14 mole percent; the balance being similar, in relative composition, to the non-a-olefin portion of Example 1.
  • the SO :olefin mole ratio in the first stage (which was carried out continuously in the reactor described in Example 1) was 1:1 and the temperature of the olefin fed to that stage was 100 F.
  • the temperature in the recycle loop was maintained at F.
  • the caustic-neutralized hydrolyzed product contained 4 to 6% of free oil, based on total organic content (dry basis).
  • Example 10 A Stage I mix made as in Example 2 was subjected to a dual extraction with pentane-water at room temperature.
  • the pentane extract was dried and concentrated under vacuum of 30 mm. HgA and cooled (on an ice bath at 010 C.) to precipitate a first crop of pure white crystals (M.P. 75 C.) which were then washed with cold pentane. From the mother liquor a second crop of pure white crystals (M.P. 62-64 C.) was obtained by further concentration of the pentane and cooling.
  • the first crop crystals had an infrared absorption spectrum as shown in FIG. 8 (a relatively quantitative diiferential spectrum taken on a solution in carbon tetrachloride) having strong absorption bands at about 7.35 and 8.63 microns, which are in the absorption ranges characteristic for sultones. There was substantially no absorption at about 7.65 microns (reported to be characteristic of delta sultones) or at about 11.2 microns. It is therefore believed that the first crop crystals represent a gamma sultone corresponding to the starting olefin (i.e., of about 18 carbon atoms).
  • the second crop crystals had an infrared spectrum as shown in FIG, 9 (taken on a melted sample squeezed into a thin solid film) which had very strong absorption at about 7.35 microns and about 7.45 microns (doublet), at about 8.45 microns and about 8.58 microns (doublet), and at about 11.05 microns and 11.2 microns (doublet), and weak absorption at about 7.65 microns. It is believed to be a delta sultone.
  • Example 10B When Example 10B was repeated, using a more highly purified sample (M.P. 79 C.) of the first crop crystals, the treatment with sodium hydroxide gave substantially complete conversion to the insoluble solid and substantially no yield of water-soluble active ingredient.
  • Example 11 A Stage 11 mix was made from the olefin described in Example 2, using, in the second stage of reaction, 5 pounds per hour of 97% H 50 and 54 pounds per hour of Stage I mix. 59 parts of the Stage II mix was frozen, held overnight, and then mixed with an additional 15 parts of 97% H 50 at 40 C. for 30 minutes and then neutralized by mixing with an excess of aqueous 15% solution of sodium hydroxide at room temperature, without heating.
  • the product was treated (as in Example 3) to form the octylamine salt, the latter was found to be substantially free of hydroxysulfonate (i.e., its content of the saturated fraction crystallizing out at room temperature was substantially zero).
  • Example 12 there were used the apparatus and process described in Example 1, with a crude 0 -0 olefin feedstock made by cracking parafiin wax and having the following analysis, as reported by the supplier:
  • Example 13 In this example, a differently constructed reactor was used for the treatment of the crude C -C olefin feedstock described in Example 12.
  • the feed rates were as follows: olefin feedstock, 40.2 lbs./hr.; 80;; 14.0 lbs./hr.
  • the S0 was supplied in air at a concentration of 4% by volume and at a pressure of 25 p.s.i.g.
  • the olefin passed continuously through the annular zone between the outer surface of a cylindrical rotor (mounted on a vertical axis) and the surrounding inner wall of a 18 anionically active ingredient and 2.9% free oil was then used for preparing a series of heavy duty built liquid detergents having the compositions shown in the following table:
  • Olefin sulfonate (proportion given is the amount of anionically active ingredient) 9 7 15 12 10 12 5 6 Potassium xylene sulfonate 8. 5 6 8. 5 8. 5 8 8 8. 5 8. 5
  • alcdhol made from three moles of ethylene oxide per mole of the alcohol (Aliol 1418 3E0) 6 Lauryl-niyristyl dimethylamine oxide 5 Why-myristio diethanolamide 2 Lauric-myristic isopropanolamide. 2
  • the outer surface of the rotor had spaced helical ridges of polytetrafluoroethylene which extended to within 0.02 inch of the cylindrical inner wall of the vessel; the clearance between the main unridged portions of the outer surface of the rotor and that inner wall was 0.2 inch; the olefin was fed in at one end of the apparatus and the sulfonated product was taken oif from the other end.
  • the reactor temperature was about 150 F.
  • the resulting Stage I mix was mixed with its weight of H 50 (supplied as 90% H SO and treated as in Example 4.
  • the neutralized product contained (on a dry basis) about 82% anionically active ingredient and about 7% free oil.
  • Example 14 A Stage II mix was produced as in Example 1, but using an olefin feedstock which contained about 88% of terminally unsaturated straight chain olefins having Example 15 270 parts of a hot neutralized slurry (having a temperature of 180 F.) produced as in Example 12 was mixed with 6% parts of an aqueous 3.75% NaOCl solution and allowed to stand for /2 hour. The product had a Klett color (measured after dilution with water to reduce its content of anionically active ingredient to 5%) of 305 as compared to a similarly measured Klett color of well over 900 for the product before NaOCl treatment. When the amount of NaOCl solution was increased to parts, the Klett color of the product was 150.
  • Example 16 The olefin feedstock of Example 14 was treated with S0 and sulfuric acid as in Example 1 and neutralized as in Example 1. The resulting neutralized product, which was a syrup containing (on an organic dry basis) 97.1%
  • formulations made from the olefin sulfonate of this example include an all-purpose liquid cleaner containing an amount of the neutralized syrup sufficient to supply 4.3% of anionically active ingredient, 3% lauricmyristic diethanolamide and 10% tetra-potassium pyrophosphate; and a dishwashing liquid containing an amount of the neutralized syrup sufficient to supply 25% of anionically active ingredient, and 3% lauric-myristic diethanolamide.
  • Example 17 Hexadecene-l, 99% pure, was treated as in Example 1, using an SO :olefin feedstock mole ratio of 1.1:1 and injecting the H (as aqueous 97% H SO continuously halfway up the tubular reactor, in amount of part of the 97% H 80 per part of Stage I mix. A sample of Stage II mix before the neutralization treatment was frozen and, within a few hours, was analyzed. The analysis showed that it contained 50.7% anionically active ingredient (determined by cationic titration of the unneutralized acidic mix).
  • the infrared absorption spectrum of the Stage II acidic mix indicated that it contained no unreacted olefin but did contain a delta sultone; comparison with the infrared spectrum of a substantially pure delta sultone isolated from a similar Stage II mix made from the same hexadecene-l feedstock indicated that the Stage II mix contained about 44% of delta sultone.
  • the 16 carbon sultone used as the reference standard was identified as a delta sultone by its IR spectrum which was characteristic of delta sultone; see the discussion in Example 10.
  • the sulfuric acid is incorporated by addition of H 80 to a substantially anhydrous Stage I mix after the initial sulfonation with 80;, has been completed. It is, however, within the broader scope of this invention to add the H 80 earlier in the process or to incorporate all or part of the desired quantity of sulfuric acid in other ways, as by the addition of an equivalent amount of water or suitable salts to react with free sulfur trioxide to form H 50 in situ.
  • the anionic active content by titration with cetyl trimethylammonium bromide, there is employed an acidified two-phase mixture containing chloroform, water, methylene blue and the material to be tested. The color concentrates almost exclusively in the lower, chloroform layer. On addition of cetyl trimethylammonium bromide or other long chain cationic reagent and agitation, the color shifts into the upper, aqueous layer; the endpoint of the titration may be taken as the point at which the lower layer is less blue than the upper layer and has a green appearance.
  • the bromine number was determined according to A.S.T.M. method D1l58-57T, modified to provide a contact time of 45 minutes instead of 40 seconds.
  • the sample dissolved in carbon tetrachloride, is treated at room temperature with an excess of bromide bromate solution in the presence of glacial acetic acid.
  • the excess bromine is reduced with potassium iodide and the liberated iodine determined by titration with sodium thiosulphate solution.
  • the improvement which comprises adding strong sulfuric acid to said reaction product to produce a mixture giving a greater yield of higher alkenyl sulfonates and a lower yield of water-insoluble free oil when tested by said treatment with hot sodium hydroxide, said olefin, said sulfonates, and said sultones containing about 8 to carbon atoms, the sulfuric acid being of at least strength and containing at most an amount of water equal to the weight of H 50 the total amount of water in the resulting mixture being less than 10% of the weight of said sulfonation reaction product.
  • said sulfonation reaction mixture is a viscous mixture produced by the continuous reaction, under substantially anhydrous conditions, of a higher alpha olefin in liquid phase with sulfur trioxide supplied as a gas diluted with at least 5 times its volume of an'inert gas, the mole ratio of sulfur trioxide to said olefin in said continuous reaction being in the range of about 0.5:1 to 13:1.
  • Process for production of a long chain anionically active sulfonic acid which comprises treating with strong sulfuric acid a long chain sultone produced by sulfonation of long chain alpha-olefin to convert said sultone to said long chain anionically active sulfonic acid, said long chain compounds containing about 8 to 30 carbon atoms, said sulfuric acid being of at least 60% strength.
  • Process for the production of a long chain anionically active sulfonic acid which comprises treating with strong sulfuric acid a preformed long chain gamma sultone to convert said sultone to said long chain anionically active sulfonic acid, said long chain compounds having about 8 to 30 carbon atoms, said sulfuric acid being of at least 60% strength, said sultone having the structure of a sultone made by reacting an alpha-olefin of 8 to 30 carbon atoms with S0 16.
  • Process for the production of a long chain anionically active sulfonic acid which comprises treating with strong sulfuric acid a preformed long chain delta sultone to convert said sultone to said long chain anionically active sulfonic acid, said long chain compounds having about 8 to 30 carbon atoms, said sulfuric acid being of at least 60% strength, said sultone having the structure of a sultone 21 made by reacting an alpha-olefin of 8 to 30 carbon atoms with S 17.
  • Process for the production of a long chain anionically active sulfonic acid which comprises treating with strong sulfuric acid a preformed mixture of a long chain gamma sultone and a long chain delta sultone to convert said sultones to said long chain anionically active sulfonic acid, said sulfuric acid being of at least 60% strength, acid sultones having the structures of gamma and delta sultones made by reacting an alpha-olefin of 8 to 30 carbon atoms with S0 18.
  • Process as set forth in claim 12 in which said sultone is present in a mixture containing unsulfonated olefin.
  • Process for the production of anionically active sulfoxy-containing acids which comprises reacting a sulfonatable alpha olefin with less than about 1 mole of sulfur trioxide per mole of olefin to produce a sultone-containing mixture and then reacting said mixture with strong sulfuric acid to convert sultone therein to alkene sulfonic acid and to produce alkyl acid sulfate, said olefin, said sultone, said acid and said sulfate each having about 8 to 30 carbon atoms, said sulfuric acid being of at least 60% strength.
  • reaction product contains gamma and delta sultones and in which the mixture produced by incorporation of sulfuric aci dcontains delta sultone, the ratio of delta sultone to gamma sultone in the latter mixture being above 1:1 and being higher than in said reaction product.

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  • General Chemical & Material Sciences (AREA)
  • Detergent Compositions (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US548827A 1965-08-04 1966-05-10 Alkene sulfonation process and products Expired - Lifetime US3428654A (en)

Priority Applications (21)

Application Number Priority Date Filing Date Title
ZA672362D ZA672362B (de) 1965-08-04
US548827A US3428654A (en) 1965-08-04 1966-05-10 Alkene sulfonation process and products
ES0328934A ES328934A1 (es) 1965-08-04 1966-07-09 Procedimiento para la fabricacion de sulfonatos de alquenilos superiores.
FR70039A FR1489920A (fr) 1965-08-04 1966-07-20 Produits détergents et leur procédé de préparation
SE10100/66A SE347256B (de) 1965-08-04 1966-07-22
CH1075566A CH491875A (de) 1965-08-04 1966-07-26 Verfahren zur Herstellung höherer Alkensulfonsäuren enthaltender Produkte, so erhaltenes Produkt und dessen Verwendung
DE1568311A DE1568311B2 (de) 1965-08-04 1966-07-27 Verfahren zur Herstellung waschaktiver höherer Alkenylsulfonate
GB34589/66A GB1166857A (en) 1965-08-04 1966-08-02 Preparation of Anionically Active Material
GB20245/69A GB1166858A (en) 1965-08-04 1966-08-02 Sulphonation of Olefins with Sulphur Trioxide
BE685012D BE685012A (de) 1965-08-04 1966-08-03
DK403866AA DK130787B (da) 1965-08-04 1966-08-04 Fremgangsmåde til fremstilling af et sulfoneringsprodukt.
JP41050842A JPS4935609B1 (de) 1965-08-04 1966-08-04
SE06929/67A SE336866B (de) 1965-08-04 1967-05-17
FR107772A FR92528E (fr) 1965-08-04 1967-05-25 Produits détergents et leur procédé de préparation
DE1617064A DE1617064B2 (de) 1965-08-04 1967-05-26 Waschmittelmischung
BE699149D BE699149A (de) 1965-08-04 1967-05-29
GB24863/67A GB1194862A (en) 1965-08-04 1967-05-30 Olefin Sulphonate Detergents
ES341149A ES341149A2 (es) 1965-08-04 1967-05-30 Procedimiento para la fabricacion de sulfonatos de alqueni-los superiores.
CH764067A CH496086A (de) 1965-08-04 1967-05-30 Waschmittelmischung
DK285067AA DK128906B (da) 1965-08-04 1967-05-31 Flydende rensemiddel.
SE15191/69A SE350507B (de) 1965-08-04 1969-11-05

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US47722865A 1965-08-04 1965-08-04
US548827A US3428654A (en) 1965-08-04 1966-05-10 Alkene sulfonation process and products
US55362266A 1966-05-31 1966-05-31

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US3428654A true US3428654A (en) 1969-02-18

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JP (1) JPS4935609B1 (de)
BE (2) BE685012A (de)
CH (2) CH491875A (de)
DE (2) DE1568311B2 (de)
DK (2) DK130787B (de)
ES (1) ES341149A2 (de)
FR (2) FR1489920A (de)
GB (3) GB1166858A (de)
SE (3) SE347256B (de)
ZA (1) ZA672362B (de)

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US3676372A (en) * 1968-10-24 1972-07-11 Chevron Res Hydrogenated olefin sulfonate-fatty acid amide detergent compositions
US3852221A (en) * 1971-08-19 1974-12-03 Jefferson Chem Co Inc Liquid olefin sulfonate detergent
US3891672A (en) * 1972-09-26 1975-06-24 Procter & Gamble Process for preparing r-sultones
US3912777A (en) * 1967-03-22 1975-10-14 Colgate Palmolive Co Use of sulfuric acid as an extractant in olefin sulfonation
US3919300A (en) * 1968-05-25 1975-11-11 Lion Fat Oil Co Ltd Detergent composition and method for preparing same
US3941834A (en) * 1971-06-09 1976-03-02 Standard Oil Company High molecular weight aliphatic hydrocarbon sulfonic acids, sulfonyl chlorides and sulfonamides
US3979340A (en) * 1973-04-09 1976-09-07 Colgate-Palmolive Company Olefin sulfonate detergent compositions
US4061586A (en) * 1973-04-09 1977-12-06 Colgate-Palmolive Company Olefin sulfonate detergent compositions
US4064076A (en) * 1973-04-09 1977-12-20 Colgate-Palmolive Olefin sulfonate detergent compositions
US4089788A (en) * 1976-06-25 1978-05-16 Standard Oil Company (Indiana) Method for improving calcium ion tolerance of hydrocarbon polymer sulfonate surfactants used in enhanced recovery processing in subterranean oil-bearing formations
US4183867A (en) * 1977-08-25 1980-01-15 The Lion Fat & Oil Co. Method for preparation of internal olefin sulfonate
US4532053A (en) * 1982-01-28 1985-07-30 Lion Corporation Micellar slug for oil recovery
US4597879A (en) * 1982-01-28 1986-07-01 Lion Corporation Micellar slug for oil recovery
US20040068133A1 (en) * 2000-12-21 2004-04-08 Edwards Charles Lee Branched primary alcohol compositions and derivatives thereof
US6747165B2 (en) 2001-02-15 2004-06-08 Shell Oil Company Process for preparing (branched-alkyl) arylsulfonates and a (branched-alkyl) arylsulfonate composition
US20040133037A1 (en) * 2001-02-15 2004-07-08 Fenouil Laurent Alain Michel Process for preparing a branched olefin, a method of using the branched olefin for making a surfactant, and a surfactant
US20040176655A1 (en) * 2003-02-05 2004-09-09 Ayoub Paul Marie Methods of preparing branched alkyl aromatic hydrocarbons
US20050101808A1 (en) * 2003-10-15 2005-05-12 Ayoub Paul M. Methods of preparing branched aliphatic alcohols
US20070225536A1 (en) * 2006-03-23 2007-09-27 Eugene Frederick Lutz Olefin conversion process and olefin recovery process
EP2217688A1 (de) * 2007-10-26 2010-08-18 Chevron Oronite Company LLC Isomerisiertes alpha-olefinsulfonat und herstellungsverfahren dafür
EP2746374A2 (de) 2012-12-21 2014-06-25 Afton Chemical Corporation Additivzusammensetzungen mit einem Reibungsmodifikator und einem Reinigungsmittel
EP2746370A1 (de) 2012-12-21 2014-06-25 Afton Chemical Corporation Reibungsmodifikatoren für Schmieröle
EP2826842A1 (de) 2013-07-18 2015-01-21 Afton Chemical Corporation Reibungsmodifikatoren für Schmieröle
EP2826843A1 (de) 2013-07-18 2015-01-21 Afton Chemical Corporation Amidalkoholreibungsmodifikatoren für Schmieröle
EP2826841A1 (de) 2013-07-18 2015-01-21 Afton Chemical Corporation Reibungsmodifikatoren für Motorenöle
US9587188B2 (en) 2013-12-17 2017-03-07 Shell Oil Company Process for preparing a branched ester and use thereof
WO2017151151A1 (en) * 2016-03-03 2017-09-08 Lockheed Martin Advanced Energy Storage, Llc Processes for forming coordination complexes containing monosulfonated catecholate ligands
US9837679B2 (en) 2014-11-26 2017-12-05 Lockheed Martin Advanced Energy Storage, Llc Metal complexes of substituted catecholates and redox flow batteries containing the same
US9877907B2 (en) 2013-02-13 2018-01-30 Kao Corporation Internal olefin sulfonate composition
US9938308B2 (en) 2016-04-07 2018-04-10 Lockheed Martin Energy, Llc Coordination compounds having redox non-innocent ligands and flow batteries containing the same
US9991544B2 (en) 2012-07-27 2018-06-05 Lockheed Martin Advanced Energy Storage, Llc Aqueous redox flow batteries comprising metal ligand coordination compounds
US9991543B2 (en) 2012-07-27 2018-06-05 Lockheed Martin Advanced Energy Storage, Llc Aqueous redox flow batteries featuring improved cell design characteristics
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US10065977B2 (en) 2016-10-19 2018-09-04 Lockheed Martin Advanced Energy Storage, Llc Concerted processes for forming 1,2,4-trihydroxybenzene from hydroquinone
US10164284B2 (en) 2012-07-27 2018-12-25 Lockheed Martin Energy, Llc Aqueous redox flow batteries featuring improved cell design characteristics
US10201488B2 (en) 2012-09-20 2019-02-12 Kao Corporation Internal olefin sulfonate composition and cleansing composition containing same
US10253051B2 (en) 2015-03-16 2019-04-09 Lockheed Martin Energy, Llc Preparation of titanium catecholate complexes in aqueous solution using titanium tetrachloride or titanium oxychloride
US10320023B2 (en) 2017-02-16 2019-06-11 Lockheed Martin Energy, Llc Neat methods for forming titanium catecholate complexes and associated compositions
US10343964B2 (en) 2016-07-26 2019-07-09 Lockheed Martin Energy, Llc Processes for forming titanium catechol complexes
EP3388504A4 (de) * 2015-12-10 2019-08-07 Kao Corporation Tensidzusammensetzung
US10377687B2 (en) 2016-07-26 2019-08-13 Lockheed Martin Energy, Llc Processes for forming titanium catechol complexes
US10497958B2 (en) 2016-12-14 2019-12-03 Lockheed Martin Energy, Llc Coordinatively unsaturated titanium catecholate complexes and processes associated therewith
US10644342B2 (en) 2016-03-03 2020-05-05 Lockheed Martin Energy, Llc Coordination complexes containing monosulfonated catecholate ligands and methods for producing the same
US10741864B2 (en) 2016-12-30 2020-08-11 Lockheed Martin Energy, Llc Aqueous methods for forming titanium catecholate complexes and associated compositions
US10930937B2 (en) 2016-11-23 2021-02-23 Lockheed Martin Energy, Llc Flow batteries incorporating active materials containing doubly bridged aromatic groups
EP3680315A4 (de) * 2017-09-06 2021-05-19 Kao Corporation Reinigungsmittelzusammensetzung für textilprodukt
WO2022046540A1 (en) * 2020-08-24 2022-03-03 University Of Kansas Haloalkane sulfonic acids, compositions thereof, and related methods

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US3819540A (en) * 1971-07-06 1974-06-25 Gulf Research Development Co Sulfonate detergents
GB8331733D0 (en) * 1983-11-28 1984-01-04 Shell Int Research Olefin sulphonate compositions
US5349101A (en) * 1992-05-28 1994-09-20 Shell Oil Company Process for the preparation of secondary alkyl sulfate-containing surfactant compositions
US5250718A (en) * 1992-09-28 1993-10-05 Shell Oil Company Process for the preparation of secondary alkyl sulfate-containing surfactant compositions
US5290484A (en) * 1992-11-12 1994-03-01 Shell Oil Company Process for the preparation of secondary alkyl sulfate-containing surfactant compositions
US5281366A (en) * 1992-09-17 1994-01-25 Shell Oil Company Process for the preparation of secondary alkyl sulfate-containing surfactant compositions
DE69314504T2 (de) * 1992-12-15 1998-02-12 Shell Int Research Sekundaralkylsulfat/zeolit-haltiges tensidgemisch und dessen herstellungsverfahren

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US2454826A (en) * 1948-11-30 Viscosity reduction of petroleum
US2691040A (en) * 1951-03-29 1954-10-05 Universal Oil Prod Co Sulfonation of organic compounds with sulfur trioxide
US3164608A (en) * 1961-12-09 1965-01-05 Henkel & Cie Gmbh Process for the preparation of sultones
US3164609A (en) * 1962-08-09 1965-01-05 Henkel & Cie Gmbh Process for the preparation of sultones

Cited By (73)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3912777A (en) * 1967-03-22 1975-10-14 Colgate Palmolive Co Use of sulfuric acid as an extractant in olefin sulfonation
US3919300A (en) * 1968-05-25 1975-11-11 Lion Fat Oil Co Ltd Detergent composition and method for preparing same
US3676372A (en) * 1968-10-24 1972-07-11 Chevron Res Hydrogenated olefin sulfonate-fatty acid amide detergent compositions
US3941834A (en) * 1971-06-09 1976-03-02 Standard Oil Company High molecular weight aliphatic hydrocarbon sulfonic acids, sulfonyl chlorides and sulfonamides
US3852221A (en) * 1971-08-19 1974-12-03 Jefferson Chem Co Inc Liquid olefin sulfonate detergent
US3891672A (en) * 1972-09-26 1975-06-24 Procter & Gamble Process for preparing r-sultones
US3979340A (en) * 1973-04-09 1976-09-07 Colgate-Palmolive Company Olefin sulfonate detergent compositions
US4061586A (en) * 1973-04-09 1977-12-06 Colgate-Palmolive Company Olefin sulfonate detergent compositions
US4064076A (en) * 1973-04-09 1977-12-20 Colgate-Palmolive Olefin sulfonate detergent compositions
US4089788A (en) * 1976-06-25 1978-05-16 Standard Oil Company (Indiana) Method for improving calcium ion tolerance of hydrocarbon polymer sulfonate surfactants used in enhanced recovery processing in subterranean oil-bearing formations
US4183867A (en) * 1977-08-25 1980-01-15 The Lion Fat & Oil Co. Method for preparation of internal olefin sulfonate
US4532053A (en) * 1982-01-28 1985-07-30 Lion Corporation Micellar slug for oil recovery
US4597879A (en) * 1982-01-28 1986-07-01 Lion Corporation Micellar slug for oil recovery
US6909020B2 (en) 2000-12-21 2005-06-21 Shell Oil Company Branched primary alcohol compositions and derivatives thereof
US7148375B2 (en) 2000-12-21 2006-12-12 Shell Oil Company Branched primary alcohol compositions and derivatives thereof
US20040073055A1 (en) * 2000-12-21 2004-04-15 Edwards Charles Lee Branched primary alcohol compositions and derivatives thereof
US20040067867A1 (en) * 2000-12-21 2004-04-08 Edwards Charles Lee Branched primary alcohol compositions and derivatives thereof
US7071364B2 (en) 2000-12-21 2006-07-04 Shell Oil Company Branched primary alcohol compositions and derivatives thereof
US20040068133A1 (en) * 2000-12-21 2004-04-08 Edwards Charles Lee Branched primary alcohol compositions and derivatives thereof
US6891056B2 (en) 2000-12-21 2005-05-10 Shell Oil Company Branched primary alcohol compositions and derivatives thereof
US20040198628A1 (en) * 2000-12-21 2004-10-07 Edwards Charles Lee Branched primary alcohol compositions and derivatives thereof
US7087777B2 (en) 2001-02-15 2006-08-08 Shell Oil Company Process for preparing a branched olefin, a method of using the branched olefin for making a surfactant, and a surfactant
US6747165B2 (en) 2001-02-15 2004-06-08 Shell Oil Company Process for preparing (branched-alkyl) arylsulfonates and a (branched-alkyl) arylsulfonate composition
US7348462B2 (en) 2001-02-15 2008-03-25 Shell Oil Company Process for preparing branched olefins from a paraffinic wax
US6765106B2 (en) 2001-02-15 2004-07-20 Shell Oil Company Process for preparing a branched olefin, a method of using the branched olefin for making a surfactant, and a surfactant
US7053257B2 (en) 2001-02-15 2006-05-30 Shell Oil Company Process for preparing (branched-alkyl) arylsulfonates and a (branched-alkyl) arylsulfonate composition
US20040133037A1 (en) * 2001-02-15 2004-07-08 Fenouil Laurent Alain Michel Process for preparing a branched olefin, a method of using the branched olefin for making a surfactant, and a surfactant
US20040167369A1 (en) * 2001-02-15 2004-08-26 Fenouil Laurent Alain Michel Process for preparing (branched-alkyl) arylsulfonates and a (branched-alkyl) arylsulfonate composition
EP1767512A2 (de) 2001-02-15 2007-03-28 Shell Internationale Researchmaatschappij B.V. Verfahren zur Herstellung eines verzweigten Olefins, Verfahren zur Verwendung des verzweigten Olefins zur Herstellung eines Tensids und Tensid
US7235684B2 (en) 2001-02-15 2007-06-26 Shell Oil Company Process for preparing (branched-alkyl) arylsulfonates and a (branched-alkyl) arylsulfonate composition
US20040176655A1 (en) * 2003-02-05 2004-09-09 Ayoub Paul Marie Methods of preparing branched alkyl aromatic hydrocarbons
US20060224028A1 (en) * 2003-02-05 2006-10-05 Ayoub Paul M Methods of preparing branched alkyl aromatic hydrocarbons
US7335802B2 (en) 2003-10-15 2008-02-26 Shell Oil Company Methods of preparing branched aliphatic alcohols
US20050101808A1 (en) * 2003-10-15 2005-05-12 Ayoub Paul M. Methods of preparing branched aliphatic alcohols
US20070225536A1 (en) * 2006-03-23 2007-09-27 Eugene Frederick Lutz Olefin conversion process and olefin recovery process
EP2217688A4 (de) * 2007-10-26 2012-01-18 Chevron Oronite Co Isomerisiertes alpha-olefinsulfonat und herstellungsverfahren dafür
EP2217688A1 (de) * 2007-10-26 2010-08-18 Chevron Oronite Company LLC Isomerisiertes alpha-olefinsulfonat und herstellungsverfahren dafür
US10056639B2 (en) 2012-07-27 2018-08-21 Lockheed Martin Energy, Llc Aqueous redox flow batteries featuring improved cell design characteristics
US10014546B2 (en) 2012-07-27 2018-07-03 Lockheed Martin Advanced Energy Storage, Llc Aqueous redox flow batteries comprising metal ligand coordination compounds
US9991543B2 (en) 2012-07-27 2018-06-05 Lockheed Martin Advanced Energy Storage, Llc Aqueous redox flow batteries featuring improved cell design characteristics
US9991544B2 (en) 2012-07-27 2018-06-05 Lockheed Martin Advanced Energy Storage, Llc Aqueous redox flow batteries comprising metal ligand coordination compounds
US10164284B2 (en) 2012-07-27 2018-12-25 Lockheed Martin Energy, Llc Aqueous redox flow batteries featuring improved cell design characteristics
US10201488B2 (en) 2012-09-20 2019-02-12 Kao Corporation Internal olefin sulfonate composition and cleansing composition containing same
EP2746374A2 (de) 2012-12-21 2014-06-25 Afton Chemical Corporation Additivzusammensetzungen mit einem Reibungsmodifikator und einem Reinigungsmittel
EP2746370A1 (de) 2012-12-21 2014-06-25 Afton Chemical Corporation Reibungsmodifikatoren für Schmieröle
US9877907B2 (en) 2013-02-13 2018-01-30 Kao Corporation Internal olefin sulfonate composition
EP2826842A1 (de) 2013-07-18 2015-01-21 Afton Chemical Corporation Reibungsmodifikatoren für Schmieröle
EP2993220A1 (de) 2013-07-18 2016-03-09 Afton Chemical Corporation Reibungsmodifikatoren für schmieröle
EP2826841A1 (de) 2013-07-18 2015-01-21 Afton Chemical Corporation Reibungsmodifikatoren für Motorenöle
EP2826843A1 (de) 2013-07-18 2015-01-21 Afton Chemical Corporation Amidalkoholreibungsmodifikatoren für Schmieröle
US9587188B2 (en) 2013-12-17 2017-03-07 Shell Oil Company Process for preparing a branched ester and use thereof
US9837679B2 (en) 2014-11-26 2017-12-05 Lockheed Martin Advanced Energy Storage, Llc Metal complexes of substituted catecholates and redox flow batteries containing the same
US10734666B2 (en) 2014-11-26 2020-08-04 Lockheed Martin Energy, Llc Metal complexes of substituted catecholates and redox flow batteries containing the same
US10253051B2 (en) 2015-03-16 2019-04-09 Lockheed Martin Energy, Llc Preparation of titanium catecholate complexes in aqueous solution using titanium tetrachloride or titanium oxychloride
CN108368455A (zh) * 2015-12-10 2018-08-03 花王株式会社 表面活性剂组合物
CN108368455B (zh) * 2015-12-10 2020-11-10 花王株式会社 表面活性剂组合物
EP3388506A4 (de) * 2015-12-10 2019-08-07 Kao Corporation Tensidzusammensetzung
EP3388504A4 (de) * 2015-12-10 2019-08-07 Kao Corporation Tensidzusammensetzung
WO2017151151A1 (en) * 2016-03-03 2017-09-08 Lockheed Martin Advanced Energy Storage, Llc Processes for forming coordination complexes containing monosulfonated catecholate ligands
US10316047B2 (en) 2016-03-03 2019-06-11 Lockheed Martin Energy, Llc Processes for forming coordination complexes containing monosulfonated catecholate ligands
US10644342B2 (en) 2016-03-03 2020-05-05 Lockheed Martin Energy, Llc Coordination complexes containing monosulfonated catecholate ligands and methods for producing the same
US9938308B2 (en) 2016-04-07 2018-04-10 Lockheed Martin Energy, Llc Coordination compounds having redox non-innocent ligands and flow batteries containing the same
US10377687B2 (en) 2016-07-26 2019-08-13 Lockheed Martin Energy, Llc Processes for forming titanium catechol complexes
US10343964B2 (en) 2016-07-26 2019-07-09 Lockheed Martin Energy, Llc Processes for forming titanium catechol complexes
US10065977B2 (en) 2016-10-19 2018-09-04 Lockheed Martin Advanced Energy Storage, Llc Concerted processes for forming 1,2,4-trihydroxybenzene from hydroquinone
US10930937B2 (en) 2016-11-23 2021-02-23 Lockheed Martin Energy, Llc Flow batteries incorporating active materials containing doubly bridged aromatic groups
US10497958B2 (en) 2016-12-14 2019-12-03 Lockheed Martin Energy, Llc Coordinatively unsaturated titanium catecholate complexes and processes associated therewith
US10741864B2 (en) 2016-12-30 2020-08-11 Lockheed Martin Energy, Llc Aqueous methods for forming titanium catecholate complexes and associated compositions
US10320023B2 (en) 2017-02-16 2019-06-11 Lockheed Martin Energy, Llc Neat methods for forming titanium catecholate complexes and associated compositions
EP3680315A4 (de) * 2017-09-06 2021-05-19 Kao Corporation Reinigungsmittelzusammensetzung für textilprodukt
RU2764033C2 (ru) * 2017-09-06 2022-01-12 Као Корпорейшн Детергентная композиция для текстильных изделий
US11634660B2 (en) 2017-09-06 2023-04-25 Kao Corporation Detergent composition for textile products
WO2022046540A1 (en) * 2020-08-24 2022-03-03 University Of Kansas Haloalkane sulfonic acids, compositions thereof, and related methods

Also Published As

Publication number Publication date
FR92528E (fr) 1968-11-22
GB1166858A (en) 1969-10-15
DK128906B (da) 1974-07-22
DE1568311B2 (de) 1975-10-30
DE1568311A1 (de) 1970-06-18
CH491875A (de) 1970-06-15
JPS4935609B1 (de) 1974-09-25
ES341149A2 (es) 1968-07-01
DE1617064B2 (de) 1975-04-17
GB1194862A (en) 1970-06-17
DK130787C (de) 1975-09-15
BE699149A (de) 1967-11-03
SE336866B (de) 1971-07-19
DK130787B (da) 1975-04-14
DE1617064A1 (de) 1971-03-18
CH496086A (de) 1970-09-15
BE685012A (de) 1967-02-03
SE350507B (de) 1972-10-30
GB1166857A (en) 1969-10-15
ZA672362B (de)
SE347256B (de) 1972-07-31
FR1489920A (fr) 1967-07-28

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